CN217600501U - Waste ionic liquid coordination treatment and recycling system - Google Patents
Waste ionic liquid coordination treatment and recycling system Download PDFInfo
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Abstract
The application provides a useless ion liquid coordination handles and resourceful system includes: a system for coordinately treating and recycling waste ionic liquid comprises: a waste ionic liquid supply device; a disruption device in fluid communication with the spent ionic liquid supply; the neutralization flocculation device is communicated with the fluid of the waste alkali liquor supply device; a displacement device for displacing the separated liquid obtained by the neutralization and flocculation device and communicating with a corresponding displacement metal supply device; a first sulfate compound reaction kettle and a second sulfate compound reaction kettle, wherein the first sulfate compound reaction kettle is communicated with the neutralization and flocculation device, and the second sulfate compound reaction kettle is communicated with the displacement device in a fluid mode; and a hydrolytic polymerization device which is communicated with the first sulfuric acid compound reaction kettle and the second sulfuric acid compound reaction kettle in a fluid mode and enables products in the first sulfuric acid compound reaction kettle and the second sulfuric acid compound reaction kettle to be subjected to hydrolytic polymerization.
Description
Technical Field
The embodiment of the application relates to a system for coordinately treating and recycling waste ionic liquid.
Background
With the rapid development of economy in China, the problem of treatment and treatment of hazardous waste becomes increasingly serious, and in recent years, the requirements of relevant national standards and laws and regulations on the treatment and treatment of hazardous waste are also becoming stricter. The problems of difficult treatment, high treatment cost and the like of waste aluminum chloride ionic liquid, waste sulfuric acid, waste alkali liquor and the like generated in the production process of a chemical plant always exist.
In the prior art, there are the following existing solutions:
NaOH (sodium hydroxide) neutralization treatment device
The utility model provides a waste ionic liquid processing apparatus, includes waste ionic liquid jar, horizontal spiral sedimentation centrifuge, clear liquid jar and sump oil recovery jar, waste ionic liquid jar's bottom discharge mouth is linked together through the feed inlet of a valve with a screw pump through the pipeline, the discharge gate of screw pump is linked together through the feed inlet of pipeline with a blender, the discharge gate of blender is linked together through the feed inlet of pipeline with horizontal spiral sedimentation centrifuge, be equipped with a slag notch in horizontal spiral sedimentation centrifuge's bottom one side, the liquid outlet of locating horizontal spiral sedimentation centrifuge bottom opposite side is linked together through the top feed inlet of pipeline with the clear liquid jar, the overflow pipe export of clear liquid jar is linked together with the feed inlet of sump oil recovery jar, the bottom discharge mouth of clear liquid jar is linked together through the feed inlet of pipeline with the blender behind a clear liquid circulating pump, be equipped with fresh alkaline liquor import and a gas vent at the top of jar.
The waste ionic liquid is treated by the reaction of the waste ionic liquid and NaOH solution, so that the components in the ionic liquid generate metal solid slag which is easy to treat, and the metal solid slag is recycled, and the environmental pollution and potential safety hazard caused by the mass storage of the waste ionic liquid are avoided.
However, the treatment process only recovers oil bodies and metal solid residues, and cannot completely treat the waste ionic liquid, and is not economical and applicable. The method can not coordinate treatment of chemical production waste sulfuric acid, waste alkali liquor and the like, is single, has higher cost, and is not suitable for large-scale chemical production.
Therefore, a system for coordinating and recycling waste ionic liquid, waste sulfuric acid and waste alkali liquor is urgently needed.
Disclosure of Invention
The method aims to solve the problems of treatment and resource utilization of waste aluminum chloride ionic liquid, waste alkali liquor and waste sulfuric acid in the process of producing alkylate by catalytic alkylation by taking C4 as a raw material. The waste ionic liquid has the characteristics of high activity, high acidity, high oil content and the like. The waste ionic liquid and the waste sulfuric acid waste alkali liquor are treated in different modes to cause resource waste, and through the method, the concentrated waste ionic liquid is subjected to coordinated treatment by a set of process, and through process design, various products with economic value such as combustible oil, metals such as copper, tin, lead and the like, flocculating agents and the like can be produced, and the method accords with relevant policies and regulations of national environmental protection and corresponding standards. The treatment process is simple under the condition of no secondary pollution, and simultaneously, the purposes of economy and applicability are achieved.
Specifically, an embodiment of the present application provides a system for coordinately treating and recycling waste ionic liquid, including: a waste ionic liquid supply device; a disruption device in fluid communication with the spent ionic liquid supply; the neutralization and flocculation device is used for neutralizing and flocculating the liquid flowing through the cracking device and is communicated with the waste lye supply device; a displacement device for displacing the separated liquid obtained by the neutralization and flocculation device and communicating with a corresponding displacement metal supply device; a first sulfuric acid compound reaction tank and a second sulfuric acid compound reaction tank, the first sulfuric acid compound reaction tank being in communication with the neutralization and flocculation device and reacting the flocculated precipitate obtained by passing through the neutralization and flocculation device, the second sulfuric acid compound reaction tank being in fluid communication with the displacement device, and wherein the first sulfuric acid compound reaction tank and the second sulfuric acid compound reaction tank are both in fluid communication with a waste sulfuric acid supply device; and a hydrolytic polymerization device which is communicated with the first sulfuric acid compound reaction kettle and the second sulfuric acid compound reaction kettle in a fluid mode and enables products in the first sulfuric acid compound reaction kettle and the second sulfuric acid compound reaction kettle to be subjected to hydrolytic polymerization, wherein the first sulfuric acid compound reaction kettle and the replacement device are communicated with the neutralization flocculation device through different pipelines.
In some embodiments, the neutralization flocculation device is further in fluid communication with the breaking device through a saltwater return system.
In some embodiments, the flocculation device obtains the flocculation precipitation and the separation liquid by sedimentation separation, and wherein a settler performing the sedimentation separation is divided into three layers, and wherein the three layers are an upper layer, a middle layer and a lower layer, wherein an oil separation plate is arranged above the upper layer of the settler and a sludge discharge port is arranged below the lower layer of the settler.
In some embodiments, the disrupting means and the neutralising flocculation device are further connected to the same combustible oil recovery device.
In some embodiments, the displacement device is further connected to the metal recovery device.
In some embodiments, the neutralization flocculation device is further connected to a flocculant supply device.
In some embodiments, the second sulfuric acid compound reaction kettle is further connected with an oxidant supply device.
In some embodiments, the hydrolytic polymerization device further comprises a heating device to apply heat during the hydrolytic polymerization reaction.
In some embodiments, the hydrolytic polymerization device is further connected to a waste phosphoric acid supply device.
In some embodiments, the spent ionic liquid in the spent ionic liquid supply comprises spent aluminum chloride ionic liquid.
In some embodiments, the first sulfuric compound reaction kettle is an aluminum sulfate reaction kettle and the second sulfuric compound reaction kettle is an iron sulfate reaction kettle.
The beneficial effect that above-mentioned technical scheme produced lies in:
(1) The whole system can effectively treat the waste ionic liquid and can make the waste ionic liquid achieve the purpose of resource utilization;
(2) The salt-containing wastewater reflux device is used, except that the starting device needs to add water, no external water supply is needed when the system runs, so that the running cost is reduced, and the waste of water resources is greatly reduced;
(3) The waste ionic liquid can be treated while various waste ionic liquids which are not easy to treat, such as waste sulfuric acid, waste alkali liquor (and waste phosphoric acid), and the like are treated;
(4) The waste ionic liquid can be subjected to innocent treatment to prepare a high-efficiency flocculant (for example, when the waste aluminum chloride ionic liquid is treated, polymeric aluminum ferric sulfate can be prepared by a hydrolytic polymerization device), and the high-efficiency flocculant can be applied to a system and can also be sold as a product;
(5) Combustible oil and metal powder (such as obtained by a replacement process) such as copper, tin, lead and the like can be collected by the combustible oil recovery device and the metal recovery device in the harmless treatment process of the waste ionic liquid, and can be sold as a product;
(6) The system has no obvious discharge of waste gas and waste ionic liquid, and does not cause pollution to the environment.
Drawings
Various aspects of the invention are best understood from the following detailed description when read with the accompanying drawing figures. It should be noted that, in accordance with standard practice in the industry, various components are not drawn to scale. In fact, the dimensions of the various elements may be arbitrarily increased or decreased for clarity of discussion.
Fig. 1 is a schematic diagram of a system for the co-ordination treatment and reclamation of waste ionic liquids according to the present application.
Detailed Description
The following disclosure provides many different embodiments, or examples, for implementing different features of the invention. Specific examples of components and arrangements are described below to simplify the present disclosure. These are, of course, merely examples and are not intended to limit the invention.
The concentrated waste ionic liquid is coordinated and treated through a set of system, various products with economic value such as combustible oil, metal powder such as copper, tin, lead and the like, flocculating agent and the like can be produced through process design, and the method conforms to relevant national environmental policy and regulation and corresponding standards. The system ensures that the treatment process is simple and simultaneously achieves the purposes of economy and applicability under the condition of not generating secondary pollution. Therefore, through the system that this application provided, can innocent treatment waste ionic liquid can reach the purpose of comprehensive utilization again, make the cost of handling harmful dangerous waste ionic liquid reduce reasonable level, accord with the requirement-innoxious, minimizing, the resourceization of national environmental protection to dangerous waste resource comprehensive utilization.
The application provides a useless ion liquid coordination handles and resourceful system specifically is:
referring to fig. 1, waste ionic liquid is supplied through a waste ionic liquid supply device, and since the waste ionic liquid contains components with strong reactivity when meeting water, the waste ionic liquid is firstly decomposed (stirring is needed, the rotating speed is 120-150 r/min) through water in a decomposing device when the waste ionic liquid is treated, and the strong reactivity is eliminated so as to facilitate subsequent treatment and resource utilization. Namely, when the equipment is started, water is added to be mixed with the waste ionic liquid for carrying out a cracking reaction, so that the waste ionic liquid loses strong reaction activity, the salt-containing water can be refluxed by a salt-containing water reflux system for carrying out the cracking reaction, water does not need to be added again, and the salt-containing water is refluxed into the waste ionic liquid = 15-20 by mass ratio during the cracking reaction by the salt-containing water reflux system.
The waste ionic liquid after flowing through the breaking device becomes broken waste ionic liquid, which further flows into the neutralization and flocculation device, i.e. in the neutralization and flocculation device, in the broken waste ionic liquidAdding waste alkali liquor through a waste alkali liquor supply device to adjust the pH value to 4-5, and generating a large amount of hydroxide floc. Since floc particles are small and the settling property is poor, which is not favorable for the subsequent filtration and dehydration operations, a flocculant is added to the neutralization reaction solution containing a large amount of hydroxide effective as an inorganic coagulant (e.g., aluminum hydroxide (Al (OH)) to improve the settling property of the neutralization solution 3 ) Therefore, it is only necessary to add an organic polymeric flocculant (e.g., PAM (polyacrylamide)) through a flocculant supply apparatus during the neutralization reaction. When Al (OH) is used 3 In addition, al (OH) 3 The pH value of the sediment ranges from 3.8 to 8.5 2 The pH of the (copper hydroxide) precipitation is in the range of 5.3 to 8.7, so that the optimum pH for the neutralization reaction is about 4 to 5, in which case Al (OH) 3 The yield of the precipitate is maximized without generating a large amount of Cu (OH) 2 Sedimentation is beneficial to the subsequent recovery and utilization of Cu (copper) through a displacement reaction, and the maximum economic value is obtained.
Further, in the neutralization flocculation apparatus, the neutralization reaction is followed by sedimentation separation (e.g., al (OH) 3 Mainly used for flocculation precipitation to enable neutralization liquid to naturally settle), the flocculation precipitation and separated liquid are obtained through sedimentation separation, oil-liquid-solid separation in a settler for sedimentation separation is divided into three layers, namely an upper layer, a middle layer and a lower layer, an oil separation baffle is arranged above the upper layer to facilitate oil-liquid separation, and a sludge discharge port is arranged below the lower layer to facilitate flocculation precipitation discharge.
The cracking reaction and the neutralization reaction generate combustible waste oil on the upper layer, and combustible oil can be obtained by recovering the combustible waste oil through a combustible oil recovery device.
In addition, one part of the separated liquid can flow back to a cracking pool in proportion according to the adding amount of the waste ionic liquid (generally, the adding amount of the waste ionic liquid is that the reflux amount of the separated liquid is = 20-50; after the rest of the separated liquid (the whole separated liquid without returning to the cracking cell) flows into the displacement means, an excessive displacement metal (e.g., 10 mass% iron powder) is added to the separated liquid by a displacement metal supply means to displace the simple metal such as copper, tin, lead, etc., and resource recovery is performed by a metal recovery means.
For flocculation precipitation (e.g., predominantly Al (OH) 3 ) Dewatering through a centrifugal filter (the rotating speed is 800-1200 r/min) to obtain a high-content flocculent precipitate (such as aluminum hydroxide), adding waste sulfuric acid through a waste sulfuric acid supply device, and generating a first sulfuric acid compound (such as aluminum sulfate) in a first sulfuric acid compound reaction kettle;
in addition, the separated liquid after passing through the displacement device is filtered (by a flocculation filtration device commonly used in the art, using a commonly used microfiltration membrane), and the separated liquid after filtration further flows into a second sulfuric acid compound reaction vessel, in which (Fe) remaining after filtration is supplied by an oxidant supply device and a waste sulfuric acid supply device 2+ Adding ferrous sulfate heptahydrate into (ferric)) ionic liquid, and adding waste sulfuric acid and H 2 O 2 Oxidizing the oxidant (hydrogen peroxide) to obtain a second sulfuric acid compound (such as ferric sulfate).
Mixing a first sulfuric acid compound (such as an aluminum sulfate solution) and a second sulfuric acid compound (such as an iron sulfate solution) in a cation molar ratio (such as Al/Fe (aluminum/iron)) of 1:8-10 in a hydrolytic polymerization device at a temperature of 60-80 ℃ (heating by a heating device) to perform hydrolytic polymerization for 30-50 minutes, and adding waste phosphoric acid serving as a stabilizer by a waste phosphoric acid supply device after the polymerization is finished, wherein H is H 3 PO 4 (phosphoric acid) can provide PO 4 3- The ions increase the molecular weight and make the prepared polymer (ferric aluminum sulfate) more stable, and Na is added 2 CO 3 (sodium carbonate) adjusting the alkalization degree (OH/Fe (hydroxyl/iron) molar ratio) to 0.2-0.4; due to Na 2 CO 3 Is easy to hydrolyze to form gas, so that in the adding process, a small amount of the mixture is introduced (for example, 0.2-0.3 mL of the mixture is added each time and added for multiple times), and the mixture is stirred at a slow speed (for example, the stirring speed is 10 r/min-20 r/min), so that the liquid is prevented from seeping out. Aging for 22-26 h to obtain polymer (such as Polymeric Aluminum Ferric Sulfate (PAFS) which can be used as flocculant).
The preparation process principle of the polymeric aluminum ferric sulfate is as follows:
Fe+H 2 SO 4 ＝FeSO 4 +H 2
2FeSO 4 +H 2 O 2 +H 2 SO 4 ＝Fe 2 (SO 4 ) 3 +2H 2 O
2Al(OH) 3 +3H 2 SO 4 ＝Al 2 (SO 4 ) 3 +6H 2 O
and (3) hydrolysis reaction:
Fe 2 (SO 4 ) 3 +Al 2 (SO 4 ) 3 +H 2 O→Fe 2 Al 2 (OH) n (SO 4 ) 3-n/2 +n/2H 2 SO 4
polymerization reaction:
m[Fe 2 Al 2 (OH) n (SO 4 ) 3-n/2 ]→[Fe 2 Al 2 (OH) n (SO 4 ) 3-n/2 ·xH 2 O]m(m≤13,1≤n≤5)
detailed description of the preferred embodiment 1
Waste ionic liquid coordination treatment and recycling system of waste aluminum chloride ionic liquid, waste sulfuric acid, waste alkali liquid and waste phosphoric acid, such as
The following:
firstly, 200 parts by weight of waste aluminum chloride ionic liquid is provided by a waste ionic liquid supply device, and 200 parts by weight of waste aluminum chloride ionic liquid and 3000 parts by weight of water are mixed in a cracking device for cracking (stirring at the rotating speed of 120-150 r/min).
300 parts by weight of waste lye is added through a waste lye supply device to carry out neutralization reaction in a neutralization flocculation device, wherein the neutralization solution contains Al (OH) with the effect of an inorganic coagulant 3 During the neutralization reaction, an appropriate amount of organic polymeric flocculant PAM is added (e.g., the solution is allowed to settle completely) by a flocculant supply device. 60 parts by weight of combustible oil produced by the cracking reaction and the neutralization reaction is collected by a combustible oil recovery device.
In the neutralization flocculation device, after the neutralization reaction, the neutralized liquid is naturally settled, a settling separator (oil-liquid solid separation) is used for separating to obtain a separated liquid and a flocculation sediment, 15 parts by weight of excessive iron powder is added into the separated liquid through a replacement metal supply device, the replacement reaction is carried out to obtain 13.5 parts by weight of metal copper (purity is 90 percent), and the metal copper is recovered through a metal recovery device.
The flocculation precipitation is centrifuged (rotation speed 800-1200 r/min, filtered (using the same equipment as the flocculation filtration) to obtain 3436 parts by weight, which is refluxed by a brine reflux system, and contains 90% Al (OH) 3 23 parts by weight of waste sulfuric acid having a sulfuric acid acidity of 30% was added through a waste sulfuric acid supply device to obtain 27 parts by weight of aluminum sulfate having a sulfuric acid acidity of 29%.
After the displacement reaction was filtered, 126.5 parts by weight of filtrate (except for the filtrate returned to the cracking tank) was obtained, 120 parts by weight of waste sulfuric acid of dilute sulfuric acid having a sulfuric acid acidity of 30% was added to the filtrate by a waste sulfuric acid supply device, and 95 parts by weight of ferrous sulfate heptahydrate, which had an iron content of 16.7% and 12 parts by weight of hydrogen peroxide having a mass concentration of 30%, was added by an oxidant supply device, to obtain 368.5 parts by weight of 17.5% ferric sulfate.
In a hydrolytic polymerization device, an aluminum sulfate solution and an iron sulfate solution are mixed in a molar ratio of 1:7 mixing, i.e. carrying out hydrolysis and polymerization for 30 minutes, and adding 64 parts by weight of waste phosphoric acid having a phosphoric acid content of 30% as a stabilizer, H, through a waste phosphoric acid supply means after completion of the polymerization 3 PO 4 Can provide PO 4 3- The ions increase the molecular weight, and a small amount of Na is added 2 CO 3 Adjusting the alkalization degree (OH/Fe molar ratio) to 0.3; due to Na 2 CO 3 Is easy to hydrolyze to form gas, so that a small amount of the water is introduced in the adding process, and the water is stirred at a low speed to avoid liquid seepage. Aging for 24h to obtain 300 parts by weight of Polymeric Aluminum Ferric Sulfate (PAFS) with the content of about 20%.
Example 2:
waste aluminum chloride ionic liquid, waste sulfuric acid, waste alkali liquid and waste phosphoric acid, and recycling method thereof
The following:
the same as in example 1, except that: in a hydrolytic polymerization unitMixing aluminum sulfate solution and ferric sulfate solution according to a molar ratio of 1:9 under the condition of a temperature of 70 ℃ (heating by a heating device), namely, carrying out hydrolysis and polymerization for 40 minutes, adding 64 parts by weight of waste phosphoric acid with a phosphoric acid content of 30% as a stabilizer by a waste phosphoric acid supply device after the polymerization is finished, and adding H 3 PO 4 Can provide PO 4 3- The ions increase the molecular weight, and a small amount of Na is added 2 CO 3 Adjusting the alkalization degree (OH/Fe molar ratio) to 0.2; due to Na 2 CO 3 Is easy to hydrolyze to form gas, so that a small amount of the water is introduced in the adding process, and the water is stirred at a low speed to avoid liquid seepage. Aging for 23h to obtain 300 parts by weight of Polymeric Aluminum Ferric Sulfate (PAFS) with the content of about 20%.
Example 3:
waste aluminum chloride ionic liquid, waste sulfuric acid, waste alkali liquid and waste phosphoric acid, and recycling method thereof
The following:
the same as in example 1, except that: in a hydrolytic polymerization device, under the condition of 80 ℃ temperature (heating by a heating device), mixing an aluminum sulfate solution and an iron sulfate solution according to a molar ratio of 1:8, namely performing hydrolysis and polymerization for 35 minutes, adding 64 parts by weight of waste phosphoric acid with 30 percent of phosphoric acid content as a stabilizer by a waste phosphoric acid supply device after the polymerization is finished, and adding H 3 PO 4 Can provide PO 4 3- The ions increase the molecular weight, and a small amount of Na is added 2 CO 3 Adjusting the alkalization degree (OH/Fe molar ratio) to 0.4; due to Na 2 CO 3 Is easy to hydrolyze to form gas, so that a small amount of the water is introduced in the adding process, and the water is stirred at a low speed to avoid liquid seepage. Aging for 26h to obtain 300 parts by weight of Polymeric Aluminum Ferric Sulfate (PAFS) with the content of about 20%.
Example 4:
waste aluminum chloride ionic liquid, waste sulfuric acid, waste alkali liquid and waste phosphoric acid, and recycling method thereof
The following:
the same as in example 1, except that: in a hydrolytic polymerization unit at a temperature of 70 DEG CUnder the condition (heating by a heating device), mixing an aluminum sulfate solution and an iron sulfate solution according to the molar ratio of 1 3 PO 4 Can provide PO 4 3- The ions increase the molecular weight, and a small amount of Na is added 2 CO 3 Adjusting the alkalization degree (OH/Fe molar ratio) to 0.3; due to Na 2 CO 3 Is easy to hydrolyze to form gas, so that a small amount of the water is introduced in the adding process, and the water is stirred at a low speed to avoid liquid seepage. Aging for 22h to obtain 300 parts by weight of Polymeric Aluminum Ferric Sulfate (PAFS) with the content of about 20%.
Example 5:
the method for coordinately treating and recycling the waste ionic liquid of the waste aluminum chloride ionic liquid, the waste sulfuric acid and the waste alkali liquor comprises the following steps:
as in example 1, no waste phosphoric acid was added through the waste phosphoric acid supplying apparatus after completion of the polymerization reaction, and only a small amount of Na was added 2 CO 3 The degree of alkalization (OH/Fe molar ratio) was adjusted to 0.3.
In the above description, unless otherwise specified, the percentages or ratios are mass ratios, and the devices used are all devices commonly used in the art (e.g., waste ionic liquid supply devices, cracking devices, etc.).
The beneficial effect that technical scheme that this application provided produced lies in:
(1) The whole system can effectively treat the waste ionic liquid and achieve the purpose of resource utilization;
(2) The salt-containing wastewater reflux device is used, except that the starting device needs to add water, no external water supply is needed when the system runs, so that the running cost is reduced, and the waste of water resources is greatly reduced;
(3) The waste ionic liquid can be treated while various waste ionic liquids which are difficult to treat, such as waste sulfuric acid, waste alkali liquor (and waste phosphoric acid), and the like are treated;
(4) The waste ionic liquid can be subjected to harmless treatment and then can be prepared into a high-efficiency flocculant (for example, when the waste aluminum chloride ionic liquid is treated, polymeric aluminum ferric sulfate can be prepared), and the high-efficiency flocculant can be applied to a system and can also be sold as a product;
(5) Combustible oil and metal powder (such as obtained by a replacement process) such as copper, tin, lead and the like can be collected by the combustible oil recovery device and the metal recovery device in the waste ionic liquid harmless treatment process and can be sold as products;
(6) The scheme has no obvious waste gas and waste ionic liquid discharge and does not cause pollution to the environment.
The foregoing has outlined features of several embodiments so that those skilled in the art may better understand the aspects of the present invention. Those skilled in the art should appreciate that they may readily use the present disclosure as a basis for designing or modifying other processes and structures for carrying out the same purposes and/or achieving the same advantages of the embodiments introduced herein. Those skilled in the art should also realize that such equivalent constructions do not depart from the spirit and scope of the present disclosure, and that they may make various changes, substitutions, and alterations herein without departing from the spirit and scope of the present disclosure.
Claims (11)
1. A system for coordinately treating and recycling waste ionic liquid is characterized by comprising:
a waste ionic liquid supply device;
a disruption device in fluid communication with the spent ionic liquid supply;
the neutralization and flocculation device is used for neutralizing and flocculating the liquid flowing through the cracking device and is communicated with the waste lye supply device;
a displacement device for displacing the separated liquid obtained by the neutralization and flocculation device and communicating with a corresponding displacement metal supply device;
a first sulfuric acid compound reaction tank and a second sulfuric acid compound reaction tank, the first sulfuric acid compound reaction tank being in communication with the neutralization and flocculation device and reacting the flocculated precipitate obtained by the neutralization and flocculation device, the second sulfuric acid compound reaction tank being in fluid communication with the displacement device, and wherein the first sulfuric acid compound reaction tank and the second sulfuric acid compound reaction tank are both in fluid communication with a waste sulfuric acid supply device; and
a hydrolytic polymerization device which is communicated with the first sulfuric acid compound reaction kettle and the second sulfuric acid compound reaction kettle in a fluid mode and enables products in the first sulfuric acid compound reaction kettle and the second sulfuric acid compound reaction kettle to be subjected to hydrolytic polymerization,
wherein the first sulfuric acid compound reaction kettle and the replacement device are communicated with the neutralization and flocculation device through different pipelines.
2. The system for the cooperative treatment and recycling of waste ionic liquids as claimed in claim 1, wherein said neutralization and flocculation device is further in fluid communication with said breaking device through a brine-containing water return system.
3. The system for coordinately treating and recycling waste ionic liquid as claimed in claim 1, wherein the flocculation device obtains the flocculation precipitation and the separation liquid through sedimentation separation, and wherein a settler performing the sedimentation separation is divided into three layers, and wherein the three layers are an upper layer, a middle layer and a lower layer, wherein an oil separation plate is arranged above the upper layer of the settler and a sludge discharge port is arranged below the lower layer of the settler.
4. The system for the coordinated treatment and recycling of waste ionic liquid as claimed in claim 1, wherein the breaking device and the neutralization flocculation device are further connected to the same combustible oil recovery device.
5. The system for the cooperative treatment and recycling of waste ionic liquid as claimed in claim 1, wherein the replacement device is further connected to a metal recovery device.
6. The system for the cooperative treatment and recycling of waste ionic liquid as claimed in claim 1, wherein the neutralization flocculation device is further connected with a flocculant supply device.
7. The system for coordinately treating and recycling waste ionic liquid as claimed in claim 1, wherein said second sulfuric acid compound reaction kettle is further connected to an oxidant supply device.
8. The system for co-ordinately processing and recycling waste ionic liquid as claimed in claim 1, wherein the hydrolytic polymerization device further comprises a heating device for heating during the hydrolytic polymerization reaction.
9. The system for the cooperative treatment and recycling of waste ionic liquid as claimed in claim 1, wherein the hydrolytic polymerization device is further connected with a supply device of waste phosphoric acid.
10. The system as claimed in claim 1, wherein the waste ionic liquid supply device comprises a waste aluminum chloride ionic liquid.
11. The system for coordinately treating and recycling waste ionic liquid as claimed in claim 10, wherein said first sulfuric acid compound reaction kettle is an aluminum sulfate reaction kettle, said second sulfuric acid compound reaction kettle is an iron sulfate reaction kettle, and a polymer generated by said hydrolytic polymerization device is a flocculant.
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